Summary of the invention
Order of the present invention mainly for the high energy consumption of gas-phase dehydration, the product dehydrate degree of depth not, device load is low, take up an area a kind of low energy consumption, the new system of automatical and efficient deep dehydration of the inferior position exploitation such as large.
Technical scheme of the present invention is: a kind of unpowered liquid phase drying system, comprising:
Absorption drying system: comprise the first adsorption dry tower in parallel and the second adsorption dry tower; First adsorption dry tower and the second drying adsorption tower have charging aperture and discharging opening respectively;
Nitrogen gas supply system: comprise source nitrogen, high temperature nitrogen branch road, nitrogen at room branch road formation, pre-dryer, high temperature nitrogen branch road is connected with source nitrogen respectively with the inlet end of nitrogen at room branch road, high temperature nitrogen branch road is connected the inlet end of pre-dryer respectively with the outlet side of nitrogen at room branch road, and the outlet side of pre-dryer is connected with the discharging opening of the first adsorption dry tower and the second adsorption dry tower respectively;
Material circulating system: comprise circulation liquid bath, circulation fluid trench bottom is connected with the charging aperture of the first adsorption dry tower and the second adsorption dry tower, and top connects the outlet side of pre-dryer;
Nitrogen purification recovery system: comprise film filter, cooler, regeneration gas liquid/gas separator, film filter has inlet end, recovery end and exhaust end, regeneration gas liquid/gas separator has feed end, outlet end and outlet side, the inlet end of film filter connects the discharging opening of the first adsorption dry tower and the second adsorption dry tower, the recovery end of film filter connects the feed end of cooler, the discharge end of cooler connects the feed end of regeneration gas liquid/gas separator, the inlet end of the outlet side junctional membrane filter of regeneration gas liquid/gas separator, the outlet end of regeneration gas liquid/gas separator connects regenerated liquid discharging tube and sends out-of-bounds.
Further, described high temperature nitrogen branch road is provided with the heater be made up of steam heater and electric heater.
Particularly, the charging aperture of the first adsorption dry tower is connected with material liquid pipe N0 by pipe N1, pipe N1 is arranged valve K1, and the discharging opening of the first adsorption dry tower is connected with production tube N24 by pipe N2, pipe N2 is arranged valve K2;
The charging aperture of the second adsorption dry tower is connected with material liquid pipe N0 by pipe N3, pipe N3 is arranged valve K3, and the discharging opening of the second adsorption dry tower is connected with production tube N24 by pipe N4, pipe N4 is arranged valve K4;
Source nitrogen connects steam heater by pipe N5, pipe N6, steam heater connects electric heater, electric heater tube connector N7, pipe N5 tube connector N8, pipe N8 tube connector N9, pipe N9 connects pre-dryer, and pre-dryer tube connector N10, pipe N10 are connected with pipe N2 and pipe N4 with valve K6 respectively by valve K5, pipe N6 is arranged valve K7, pipe N8 is arranged valve K8, pipe N9 is arranged valve K9, pipe N10 is arranged valve K10;
Circulation fluid trench bottom tube connector N11, pipe N11 tube connector N12 and pipe N13, pipe N12 is connected with pipe N1 and pipe N3 with valve K12 respectively by valve K11, pipe N11 is arranged valve K13, tube connector N14 and pipe N15 is distinguished after pipe N13 being arranged valve K14, the recovery end of pipe N15 junctional membrane filter, circulation liquid bath top tube connector N16, pipe N16 is tube connector N17 and pipe N18 respectively, pipe N16 is arranged valve K15, pipe N17 is arranged valve K16 and the inlet end of junctional membrane filter, pipe N18 connects the outlet side of regeneration gas liquid/gas separator after connecting valve K17, the outlet end of regeneration gas liquid/gas separator arranges valve K19, pipe N15 is arranged valve K20, pipe N14 connects the feed end of cooler, the discharge end of cooler connects the feed end of regeneration gas liquid/gas separator by pipe N19,
Pipe N20 one end is connected with pipe N2 and pipe N4 with valve K23 respectively by valve K22, and the pipe N20 other end is tube connector N21 and pipe N22 respectively, pipe N22 is arranged valve K18 and is connected with pipe N17; Pipe N10 is connected with pipe N16 by valve K24.
Technique is described as: liquid to be dried carries out adsorption drying process from the first adsorption dry tower, and the second adsorption dry tower carries out desorption and regeneration process, material liquid pipe topping up all the time, and after the topping up drying all the time of product pipe, product sends battery limit (BL) by pipeline.
Meanwhile, the second adsorption dry tower has adsorbed, and enters discharge opeing, and liquid is pressed into circulation liquid bath by nitrogen at room.In latter stage, the liquid of small part, through cooler, is kept in regeneration gas liquid/gas separator; And continue to pass into nitrogen and purge a period of time, guarantee to heat in front tower without liquid material.After discharge opeing, purging terminate, high temperature nitrogen is filled with from against absorption direction through Steam Heating and electrically heated high temperature nitrogen, carry out intensification to adsorbent to resolve, pyrolysis gassing is kept in regeneration gas liquid/gas separator through cooler condensation reclaiming liquid, break for preventing adsorbent steep temperature rise from causing, by temperature adjustment by-pass, electric heater optimum configurations, progressively promote nitrogen temperature.After bed outlet temperature reaches regulation, continue little tolerance and pass into maintenance temperature a period of time, thoroughly that regenerating molecular sieve is complete.After intensification terminates, be filled with nitrogen at room, adsorption bed is lowered the temperature.After cooling terminates, be filled with nitrogen in bed, before passing into liquid charging stock, need the second adsorption dry tower to be full of liquid.Adopt nitrogen at room to squeeze in tower by the feed liquid in circulation liquid bath at the bottom of the second adsorption dry tower tower, tower top is vented, and sends battery limit (BL) through membrane module nitrogen purge gas, reclaim organic matter and return regeneration gas liquid/gas separator, meanwhile, keep the certain liquid level of regeneration gas liquid/gas separator, the organic of recovery is sent battery limit (BL).According to the actual topping up situation of the second adsorption dry tower, supplement appropriate material liquid.So far, the second adsorption dry tower the first adsorption dry tower carry out adsorption dry terminate before ready, wait to be switched, enter next complete adsorption drying process.
The present invention compared with prior art tool has the following advantages:
The liquid-phase product dehydration degree of depth is good, can reach ppm level; Equipment takes up an area little, can meet large load and produce; Unpowered equipment, invest little, operating cost is low; Abundant recovery nitrogen, energy consumption is low, and plant running is stablized, and product recovery rate is high, purity is high.
Embodiment 1
As shown in Figure 1, a kind of unpowered liquid phase drying system, comprising:
Absorption drying system: comprise the first adsorption dry tower 1 and the second adsorption dry tower 2 in parallel; First adsorption dry tower 1 and the second drying adsorption tower have charging aperture and discharging opening respectively;
Nitrogen gas supply system: comprise source nitrogen, high temperature nitrogen branch road, nitrogen at room branch road formation, pre-dryer 4, high temperature nitrogen branch road is connected with source nitrogen respectively with the inlet end of nitrogen at room branch road, high temperature nitrogen branch road is connected the inlet end of pre-dryer 4 respectively with the outlet side of nitrogen at room branch road, and the outlet side of pre-dryer 4 is connected with the discharging opening of the first adsorption dry tower 1 and the second adsorption dry tower 2 respectively; Described high temperature nitrogen branch road is provided with the heater be made up of steam heater 6 and electric heater 5.
Material circulating system: comprise circulation liquid bath 3, is connected with the charging aperture of the first adsorption dry tower 1 and the second adsorption dry tower 2 bottom circulation liquid bath 3, and top connects the outlet side of pre-dryer 4;
Nitrogen purification recovery system: comprise film filter 9, cooler 7, regeneration gas liquid/gas separator 8, film filter 9 has inlet end, recovery end and exhaust end, regeneration gas liquid/gas separator 8 has feed end, outlet end and outlet side, the inlet end of film filter 9 connects the discharging opening of the first adsorption dry tower 1 and the second adsorption dry tower 2, the recovery end of film filter 9 connects the feed end of cooler 7, the discharge end of cooler 7 connects the feed end of regeneration gas liquid/gas separator 8, the inlet end of the outlet side junctional membrane filter 9 of regeneration gas liquid/gas separator 8, the outlet end of regeneration gas liquid/gas separator 8 connects regenerated liquid discharging tube and sends out-of-bounds.
Particularly, system architecture of the present invention is described with reference to the accompanying drawings:
The charging aperture of the first adsorption dry tower 1 is connected with material liquid pipe N0 by pipe N1, pipe N1 is arranged valve K1, and the discharging opening of the first adsorption dry tower 1 is connected with production tube N24 by pipe N2, pipe N2 is arranged valve K2;
The charging aperture of the second adsorption dry tower 2 is connected with material liquid pipe N0 by pipe N3, pipe N3 is arranged valve K3, and the discharging opening of the second adsorption dry tower 2 is connected with production tube N24 by pipe N4, pipe N4 is arranged valve K4;
Source nitrogen connects steam heater 6 by pipe N5, pipe N6, steam heater 6 connects electric heater 5, electric heater 5 tube connector N7, pipe N5 tube connector N8, pipe N8 tube connector N9, pipe N9 connects pre-dryer 4, and pre-dryer 4 tube connector N10, pipe N10 are connected with pipe N2 and pipe N4 with valve K6 respectively by valve K5, pipe N6 is arranged valve K7, pipe N8 is arranged valve K8, pipe N9 is arranged valve K9, pipe N10 is arranged valve K10;
Tube connector N11 bottom circulation liquid bath 3, pipe N11 tube connector N12 and pipe N13, pipe N12 is connected with pipe N1 and pipe N3 with valve K12 respectively by valve K11, pipe N11 is arranged valve K13, tube connector N14 and pipe N15 is distinguished after pipe N13 being arranged valve K14, the recovery end of pipe N15 junctional membrane filter 9, circulation liquid bath 3 top tube connector N16, pipe N16 is tube connector N17 and pipe N18 respectively, pipe N16 is arranged valve K15, pipe N17 is arranged valve K16 and the inlet end of junctional membrane filter 9, pipe N18 connects the outlet side of regeneration gas liquid/gas separator 8 after connecting valve K17, the outlet end of regeneration gas liquid/gas separator 8 arranges valve K19, pipe N15 is arranged valve K20, pipe N14 connects the feed end of cooler 7, the discharge end of cooler 7 connects the feed end of regeneration gas liquid/gas separator 8 by pipe N19,
Pipe N20 one end is connected with pipe N2 and pipe N4 with valve K23 respectively by valve K22, and the pipe N20 other end is tube connector N21 and pipe N22 respectively, pipe N22 is arranged valve K18 and is connected with pipe N17; Pipe N10 is connected with pipe N16 by valve K24.
Operation control procedure of the present invention is as follows:
Absorption phase: during dry operation, the first adsorption dry tower 1 carries out adsorption drying process, and the second adsorption dry tower 2 carries out desorption and regeneration process, material liquid pipe N0 topping up all the time, product pipe N24 topping up all the time, now, the only main valve K1 that first adsorption dry tower 1 associates, K2 opens, and other valve cuts out.Main process stream is through N0, K1, N1, and 1, N2, K2, N24, product goes out battery limit (BL).
Blowdown period: meanwhile, the second adsorption dry tower 2 has adsorbed, and enters discharge opeing, closes K3, K4, K23, K24, K14 opens K8, K9, and 10, K6, K12, K13, K15, K16, K20, K17, nitrogen at room enters the second adsorption dry tower 2 through valve K8 from N4, and the liquid in the second adsorption dry tower 2 is pressed into circulation liquid bath 3 from N3, N12, N11.In latter stage, close K13, open K14, other valve is remained stationary, and the liquid of small part is through K14, N13, N14, and cooler 7, N19, keeps in regeneration gas liquid/gas separator 8; And continue to pass into nitrogen and purge a period of time, guarantee to heat in front tower without liquid material.
The heated constant temperature stage: after discharge opeing, purging terminate, open K7 and close K8, other valve is remained stationary, high temperature nitrogen is filled with from against absorption direction through Steam Heating and electrically heated high temperature nitrogen, carry out intensification to adsorbent to resolve, breaking for preventing adsorbent steep temperature rise from causing, by temperature adjustment by-pass, electric heater optimum configurations, progressively promoting nitrogen temperature.After bed outlet temperature reaches setting, continue little tolerance and pass into maintenance temperature a period of time, thoroughly that regenerating molecular sieve is complete.
Temperature-fall period: after intensification terminates, other valve is remained stationary, and opens K7 and closes K8, continues to be filled with nitrogen at room along against absorption direction, lowers the temperature to adsorption bed.After cooling terminates, in bed, be filled with nitrogen.
The topping up stage: after cooling terminates, be filled with nitrogen in bed, before passing into liquid charging stock, need the second adsorption dry tower 2 to be full of liquid.Under temperature-fall period valve state, close K6, K16, KK14, opens k23, k18, k19 adopts nitrogen at room to squeeze in tower by the feed liquid in circulation liquid bath 3 at the bottom of the second adsorption dry tower 2 tower, tower top is vented, and sends battery limit (BL) through membrane module nitrogen purge gas, reclaims organic matter and returns regeneration gas liquid/gas separator 8, simultaneously, according to its liquid level, regulating valve k19 aperture, sends battery limit (BL) by the organic of recovery.According to the actual topping up situation of the second adsorption dry tower 2, supplement appropriate material liquid.
So far, the second adsorption dry tower 2 the first adsorption dry tower 1 carry out adsorption dry terminate before ready, wait to be switched, enter next complete adsorption drying process.
The above embodiment only have expressed the detailed description of the invention of the application, and it describes comparatively concrete and detailed, but therefore can not be interpreted as the restriction to the application's protection domain.It should be pointed out that for the person of ordinary skill of the art, under the prerequisite not departing from technical scheme design, can also make some distortion and improvement, these all belong to the protection domain of the application.